WO2005099896A1 - Solide acid catalyst and method of using same - Google Patents

Solide acid catalyst and method of using same Download PDF

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Publication number
WO2005099896A1
WO2005099896A1 PCT/US2005/011659 US2005011659W WO2005099896A1 WO 2005099896 A1 WO2005099896 A1 WO 2005099896A1 US 2005011659 W US2005011659 W US 2005011659W WO 2005099896 A1 WO2005099896 A1 WO 2005099896A1
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Prior art keywords
catalyst
catalyst composition
group
oxide
fumed silica
Prior art date
Application number
PCT/US2005/011659
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English (en)
French (fr)
Inventor
Jinsuo Xu
Chuen Y. Yeh
Philip J. Angevine
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Abb Lummus Global, Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Abb Lummus Global, Inc. filed Critical Abb Lummus Global, Inc.
Priority to EP05767598A priority Critical patent/EP1735092A1/en
Priority to CA2560339A priority patent/CA2560339C/en
Priority to KR1020067021183A priority patent/KR101114242B1/ko
Priority to CN2005800110655A priority patent/CN1968747B/zh
Priority to BRPI0508644-2A priority patent/BRPI0508644B1/pt
Priority to JP2007508387A priority patent/JP4675956B2/ja
Publication of WO2005099896A1 publication Critical patent/WO2005099896A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/652—Chromium, molybdenum or tungsten
    • B01J23/6527—Tungsten
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    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
    • C07C5/2767—Changing the number of side-chains
    • C07C5/277—Catalytic processes
    • C07C5/2772—Catalytic processes with metal oxides
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C10G45/62—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/02—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used
    • C10G49/04—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used containing nickel, cobalt, chromium, molybdenum, or tungsten metals, or compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/063—Titanium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/066—Zirconium or hafnium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/652—Chromium, molybdenum or tungsten
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    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
    • B01J27/053—Sulfates
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
    • B01J27/057—Selenium or tellurium; Compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
    • C07C2523/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals combined with metals, oxides or hydroxides provided for in groups C07C2523/02 - C07C2523/36
    • C07C2523/56—Platinum group metals
    • C07C2523/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tatalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/652—Chromium, molybdenum or tungsten
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1081—Alkanes
    • C—CHEMISTRY; METALLURGY
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    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention relates to a catalyst for use in hydrocarbon conversion processes, and more particularly to the preparation of anion modified solid acid catalysts.
  • oxides such as 0 3 /Zr0 2 , S0 4 - 2 /Zr0 2 , Mo0 3 /Zr0 2 , S0 4 "2 /Ti0 2 , and S0 4 " 2 /Sn0 2 , are strong solid acids and have shown promising
  • a solid acid catalyst comprising a compound of anion-modified metal oxide doped with metal ions and a method of isomerizing an alkane using the catalyst.
  • Catalysts prepared in accordance with prior art methods are in powder form and are not suitable for loading into most of the commercial reactors, which require catalysts formed into granules, spheres or extrudates with good mechanical strength while retaining high activity.
  • the solid acid catalysts mentioned above can be admixed with binders such as alumina, clay, or silica to provide shaped catalyst particles with good mechanical strength.
  • binders such as alumina, clay, or silica
  • the catalyst composition is advantageously employed in hydrocarbon conversion processes such as isomerization, catalytic cracking, alkylation and ' transalkylation.
  • the present invention employs fumed silica as a binder component for the shaping of powder mixed oxide catalysts to achieve a shaped catalyst with excellent physical strength and enhanced catalyst performance for alkane isomerization.
  • the final shape of the catalyst can be, for example, an extrudate, sphere, or tablet.
  • the catalyst of the present invention comprises an oxygen compound of one or more elements of Group IVA or IVB (CAS notation) of the Periodic
  • Group IVB elements include titanium (Ti) , zirconium (Zr) and hafnium (Hf) .
  • Group IVA elements include titanium (Ti) , zirconium (Zr) and hafnium (Hf) .
  • Group VIB or Group VIA element of the Period Table include chromium (Cr) , molybdenum (Mo) and tungsten ( ) .
  • Group VIA elements include sulfur (S) , selenium (Se) and tellurium (Te) .
  • Group VIB or VIA compound can typically range from about 0.001 to 1000, preferably 0.1 to about 100, and more preferably from about 1 to about 10.
  • Preferred catalyst combinations include, for example, 0 3 /Zr0 2/ S0 4 " 2 /Zr0 2 ,
  • the catalyst can be modified by the inclusion of a dopant selected from compounds of aluminum, gallium, cerium, antimony, scandium, magnesium, cobalt, iron, chromium, yttrium and/or indium.
  • the catalyst includes an aluminum doped zirconia combined with tungsten oxide, designated as W0 3 /Al-Zr0 2 .
  • the catalyst can also include a Group VIII noble metal component such as platinum, palladium or iridium.
  • the binder of the present invention contains fumed-. silica. Fumed silica is prepared by the vapor phase
  • halosilane e.g., silicon tetrachloride
  • the combustion process produces silicon dioxide molecules ' which condense to form particles.
  • the particles collide and sinter together.
  • the primary particles have a diameter ranging from about 9 nm to about
  • Fumed silica is amorphous.
  • the individual particles are non- porous.
  • the agglomerates have a very high void volume (>98%) .
  • the BET surface area of fumed silica typically ranges from about 160 m 2 /g to about 200 m 2 /g.
  • Fumed silica suitable for use in the invention can be obtained under the designation AEROSIL ® from Degussa Co. ' , or under the designation CAB-O-SIL ® from the Cabot Corporation. As shown below, fumed silica provides surprisingly better results for alkane isomerization as compared with other
  • silica or alumina binders At least about 1% by weight of fumed silica is incorporated into the final mixed
  • colloidal silica includes amorphous silica particles having a size usually of less than about 100 microns.
  • the aggregate particle size can be as small as the size of he- primary particles.
  • the surface of the colloidal silica particles typically consists of silanols having hydroxyl groups attached to the silicon atoms, e.g., Si-(OH) x , or siloxanes, e.g., Si-O-Si-0-.
  • Colloidal silica is typically produced by adjusting the pH of a sodium silicate solution, for example by cation exchange, to form a silica sol.
  • the feedstock for the present process may be one which contains significant amounts of C 5 + normal and/or slightly branched paraffins.
  • the feedstock may contain monocyclic aromatic compounds and/or cyclic paraffins, such as cyclohexane .
  • the present catalyst may be. used to isomerize C 4 -C 8
  • paraffin hydrocarbons either as pure compounds or mixtures.
  • the isomerization is carried out in the presence of the
  • reaction temperatures are suitably in the range of about 77°F to 800 °F (about 25°C to 425 °C) . Temperatures outside this range may be utilized although they are normally less
  • Typical temperatures range from about 200°F to 600°F (about 43°C to 316°C) .
  • Pressures can typically range from about 1 psig up to about 1,500 psig (about 7,000 kPa) , although higher pressures can also be used.
  • Lower pressures, in the range of about 50 to 500 psig (about 350 kPa to 3,500kPa) may readily be employed; and the use of relatively low pressures within this range will generally be preferred in order to permit the use of low pressure equipment .
  • the isomerization is usually carried out in the presence of hydrogen, typically at a molar ratio relative to the feed from 0.01 to 10:1 and usually from 0.5:1 to 2:1.
  • An aluminum-doped mixed oxide catalyst containing a platinum component was prepared in accordance with the following procedure .
  • the product was a yellowish powder of tungstated aluminum doped zirconia
  • the shaped catalyst was formed by combining the tungstated aluminum doped zirconia with 'the binder, shaping and then calcining, as indicated. To incorporate the noble metal into this material the tungstated aluminum doped zirconia was impregnated with
  • the amount of catalyst/binder sample varied according to the amount of binder, but in all cases the total amount of active W0 3 /Al-Zr0 2 was maintained at about 500 mg.
  • the catalyst was loaded into a % inch o.d. quartz tube reactor with a thermocouple located below the
  • the catalyst bed was heated in flowing helium with a 10°C/min ramp rate to 350°C and held for 60 minutes. Then the helium flow was replaced with hydrogen, and the
  • This comparative example illustrates the preparation and performance- testing of tungstated aluminum-doped zirconia with platinum added. No binder was employed. 18 Parts of the material obtained from example 1 was impregnated with 6.21 parts of 1.74wt% of (NH 3 ) 4 Pt (N0 3 ) 2 aqueous solution. After calcination at 350 C for 3 hours, the platinum salt decomposed into platinum oxide. The sample was designated as 0.6% Pt/W0 3 /Al-Zr0 2 and used for the performance test described above. The results are shown in Table 1. COMPARATIVE EXAMPLE 2 This comparative example illustrates the preparation and performance- testing of tungstated aluminum-doped zirconia with platinum added. No binder was employed. 18 Parts of the material obtained from example 1 was impregnated with 6.21 parts of 1.74wt% of (NH 3 ) 4 Pt (N0 3 ) 2 aqueous solution. After calcination at 350 C for 3 hours, the platinum salt decomposed into
  • the Pt/W0 3 /Al-Zr0 2 catalyst was prepared in accordance with Comparative Example 1 except that the platinum content was adjusted to 1.0 wt% .
  • a shaped catalyst with 80% mixed-oxide/20% alumina was prepared by mixing 8.0 parts of Pt/W0 3 /Al-Zr0 2 prepared according to Comparative Example 1 and 10.0 parts of Nyacol colloidal alumina (20% alumina in aqueous medium) . The mixture was pressed in a "dough-like" form and subsequently calcined.
  • COMPARATIVE EXAMPLE 3 This comparative example illustrates the preparation and isomerization performance characteristics of colloidal silica-bound mixed oxide catalyst.
  • the Pt/W0 3 /Al-Zr0 2 catalyst was prepared in accordance with Comparative Example 1 to provide 0.6% Pt.
  • a colloidal silica source containing 40 wt% Si0 2 in an aqueous medium (Nalco-2327) was obtained from ONDEO Nalco Company, Chicago, IL. Two parts of 0.6% Pt/W0 3 /Al-Zr0 2. prepared in Comparative Example 1 was mixed
  • COMPARATIVE EXAMPLE 4 This comparative example illustrates the preparation and isomerization performance characteristics of Boehmite alumina-bound mixed oxide catalyst. The platinum was added after shaping.
  • Catapal ® "D" alumina (Boehmite) was obtained from SASOL North American Inc. Two hundred seventy two (272) parts of W0 3 /Al-Zr0 2 prepared according to the procedure set forth above, was mixed with 117 parts of Catapal ® "D” alumina, 135 parts of deionized water, and 3.13 parts of 70% nitric acid. The mixture was mixed in a mixing devise thoroughly, and then transferred into the cylinder of- a hydraulics extruder (Loomis Ram Extruder, Mpdel 232-16) followed with extrusion into 1/16" diameter extrudates .
  • the platinum was added after shaping.
  • Catapal ® "D" alumina (Boehmite) was obtained from SASOL North American Inc. Two hundred seventy
  • extrudates were calcined under the following conditions : static air, 90°C for 1 hour; 120°C for 1 hour, raised to
  • COMPARATIVE EXAMPLE 5 This comparative example illustrates the preparation and isomerization performance characteristics- of precipitated silica-bound mixed oxide catalyst.
  • the Pt/W0 3 /Al-Zr0 2 catalyst was prepared in accordance with Comparative Example 1 to provide 0.6% Pt .
  • Precipitated silica Hi-Sil 233 was obtained from PPG Industries Inc., Pittsburg, PA. This Hi-Sil 233 silica contains 0.55 wt% Na. Since Na could significantly deteriorate the catalyst acidity, the "as is" Hi-Sil 233 was washed thoroughly to lower the Na level below 300 ppm prior to mixing with the
  • W0 3 /Al-Zr0 2 powder 2.4 Parts of W0 3 /Al-Zr0 2 were mixed with 0.6 parts of washed Hi-Sil 233. The mixture was pressed in a "dough-like" form and subsequently calcined. The calcination conditions were: static air, 120 D C for 6 hours, raised to 450°C with ramp rate of 5°C/min and held for 5 hours, and cooled to room temperature. The mechanical
  • EXAMPLE 1 This example illustrates the preparation and isomerization performance characteristics of the fumed silica-bound mixed oxide catalyst of the present invention. The platinum was incorporated into the catalyst prior to shaping. AEROSIL ® brand fumed Si0 2 (AEROSIL 200) was obtained from Degussa Corporation. 2.4 ' Parts of 0.6% Pt/W0 3 /Al-Zr0 2 prepared in Comparative Example 1 was mixed with 0.11 parts of AEROSIL 200 and 0.28 parts of deionized
  • the mixture was pressed in a "dough-like" form and subsequently calcined.
  • the calcination conditions were: static air, 90 °C for 1 hour, 120°C for 1 hour, raised to 450°C with a ramp rate of 5°C/min and held for 5 hours, cooled to room temperature.
  • the material was pulverized to a fine powder and used for isomerization performance
  • AEROSIL ® Si0 2 (AEROSIL 200) was obtained from Degussa Corporation. 7.2 Parts .of 0 3 /Al-Zr0 2 was mixed with ' 0.33 - parts of AEROSIL 200 and 2'.75 parts of deionized water. The mixture was pressed in a "dough-like" form and subsequently calcined. The calcination conditions were: static air, 120°C for 1 hour, raised to 450°C with ramp rate of 5°C/min and held for 5 hours.
  • Example 4 This example illustrates the preparation and isomerization performance characteristics of the fumed silica bound mixed oxide catalyst of the present invention.
  • AEROSIL ® Si0 2 (AEROSIL 200) was obtained from Degussa Corporation.. 8.0
  • AEROSIL 200 and -180 parts of deionized water.
  • the mixture was mixed in a mixing devise thoroughly, and then transferred into the cylinder of a hydraulics extruder (Loomis Ram Extruder, Model 232-16) followed with extrusion into 1/16" diameter extrudates.
  • the calcination conditions for the extrudates were: static air, 120°C, raised to 450°C with a ramp rate of 10°C/min and held for 5 hours. This calcined extrudates has crush strength of 1.9 lb/mm
  • the shaped catalyst using precipitated silica as binder has low mechanical strength but exhibits fair isomerization activity (Comparative Example 5) .
  • Fumed silica has lower surface density of hydroxyl groups than precipitated silica and colloidal - silica, therefore the interaction between fumed silica and Pt/W0 3 /Al-Zr0 2 will be relatively weaker. Strong interaction may reduce the acidity of the catalyst.

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KR1020067021183A KR101114242B1 (ko) 2004-04-14 2005-04-06 고체산 촉매 및 그 사용방법
CN2005800110655A CN1968747B (zh) 2004-04-14 2005-04-06 固体酸催化剂及其使用方法
BRPI0508644-2A BRPI0508644B1 (pt) 2004-04-14 2005-04-06 Composição de catalisador compreendendo partículas de sílica fumigada e processo de conversão química de hidrocarbonetos
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EP2801564A1 (de) 2013-05-06 2014-11-12 LANXESS Deutschland GmbH Decarboxylirung von 6-Methylsalicylsäure
FR3128132A1 (fr) * 2021-10-19 2023-04-21 IFP Energies Nouvelles Catalyseur comprenant un oxyde de zirconium sulfaté dopé

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CN106140197B (zh) * 2015-03-24 2019-03-12 中国石油天然气股份有限公司 固体超强酸催化剂及其制备方法及轻质正构烷烃的异构化方法
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CN106215969B (zh) * 2016-07-25 2018-08-21 江苏大学 一种铈掺杂固体超强酸催化剂及其制备方法
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EP4234591A3 (en) 2018-09-17 2023-09-27 Chevron Phillips Chemical Company LP Light treatment of chromium catalysts and related catalyst preparation systems and polymerization processes
US11396485B2 (en) 2019-09-16 2022-07-26 Chevron Phillips Chemical Company Lp Chromium-based catalysts and processes for converting alkanes into higher and lower aliphatic hydrocarbons
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CN113731436B (zh) * 2020-05-27 2023-10-13 中国石油化工股份有限公司 一种具有芳构化功能的脱硫催化剂及其制备方法和烃油脱硫方法
CN113731435B (zh) * 2020-05-27 2023-10-10 中国石油化工股份有限公司 一种降烯烃脱硫催化剂及其制备方法和烃油脱硫方法
WO2022056146A1 (en) 2020-09-14 2022-03-17 Chevron Phillips Chemical Company Lp Transition metal-catalyzed production of alcohol and carbonyl compounds from hydrocarbons
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WO2008018970A2 (en) * 2006-08-03 2008-02-14 Abb Lummus Global Inc. Doped solid acid catalyst composition, process of conversion using same and conversion products thereof
WO2008018970A3 (en) * 2006-08-03 2008-05-29 Abb Lummus Global Inc Doped solid acid catalyst composition, process of conversion using same and conversion products thereof
JP2009545436A (ja) * 2006-08-03 2009-12-24 ラマス テクノロジ インコーポレイテッド ドープされた固体酸触媒組成物、そのドープされた固体酸触媒組成物を用いた変換プロセス、およびその変換生成物
EP2801564A1 (de) 2013-05-06 2014-11-12 LANXESS Deutschland GmbH Decarboxylirung von 6-Methylsalicylsäure
WO2014180838A1 (de) 2013-05-06 2014-11-13 Lanxess Deutschland Gmbh Decarboxylierung von 6-methylsalicylsäure
FR3128132A1 (fr) * 2021-10-19 2023-04-21 IFP Energies Nouvelles Catalyseur comprenant un oxyde de zirconium sulfaté dopé
WO2023066714A1 (fr) * 2021-10-19 2023-04-27 IFP Energies Nouvelles Catalyseur comprenant un oxyde de zirconium sulfaté dopé

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RU2006140090A (ru) 2008-05-20
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RU2338589C2 (ru) 2008-11-20
BRPI0508644B1 (pt) 2014-10-14
KR101114242B1 (ko) 2012-04-16
US7304199B2 (en) 2007-12-04
CN101797503A (zh) 2010-08-11
JP4675956B2 (ja) 2011-04-27
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